BIOREACTOR FOR SYNGAS FERMENTATION

Abstract

A bioreactor is provided that includes a main reactor having a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor. The bioreactor also includes a growth reactor continuous with the main reactor and having a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor. A method is also provided where acetogenic bacteria are contacted with syngas in a growth fermentor section of a reactor vessel that is continuous with a main fermentor section of a reactor vessel.

Description

This application claims the benefit of U.S. Provisional Application Nos. 61/571,564 and 61/571,565, both filed Jun. 30, 2011 and 61/573,845, filed Sep. 13, 2011, all of which are incorporated in their entirety herein by reference.

A process and bioreactor are provided for syngas fermentation. More specifically, the bioreactor includes a growth reactor section continuous with a main reactor section.

BACKGROUND

Anaerobic microorganisms can produce ethanol from carbon monoxide (CO) through fermentation of gaseous substrates. Fermentations using anaerobic microorganisms from the genus Clostridium produce ethanol and other useful products. For example, U.S. Pat. No. 5,173,429 describes Clostridium ljungdahlii ATCC No. 49587, an anaerobic microorganism that produces ethanol and acetate from synthesis gas. U.S. Pat. No. 5,807,722 describes a method and apparatus for converting waste gases into organic acids and alcohols using Clostridium ljungdahlii ATCC No. 55380. U.S. Pat. No. 6,136,577 describes a method and apparatus for converting waste gases into ethanol using Clostridium ljungdahlii ATCC No. 55988 and 55989.

The CO is often provided to the fermentation as part of a gaseous substrate in the form of a syngas. Gasification of carbonaceous materials to produce producer gas or synthesis gas or syngas that includes carbon monoxide and hydrogen is well known in the art. Typically, such a gasification process involves a partial oxidation or starved-air oxidation of carbonaceous material in which a sub-stoichiometric amount of oxygen is supplied to the gasification process to promote production of carbon monoxide as described in WO 2009/154788.

Fermentation of gaseous substrates can be challenging because at least a portion of the gaseous substrate must dissolve in an aqueous fermentation broth before the substrate can be metabolized by the microbial culture. Fermentations where the gaseous substrate provides the carbon and energy source for the microorganism are particularly challenging due to the large amount of substrate needed to be solubilized in the fermentation broth before metabolism can take place. Substrates such as CO which have a low solubility in an aqueous fermentation broth require a highly efficient mass transfer into an aqueous fermentation broth as the CO provides a carbon source for the anaerobic fermentation. Attempts to improve CO mass transfer are described in U.S. Pat. Nos. 5,972,661 and 7,201,884 and in WO 2011/028137.

Fermentation processes with acetogenic bacteria typically include one or more seed reactors, one or more growth reactors and at least one main reactor. Acetogenic bacteria are normally grown to a certain cell density in a seed reactor. The seed reactor is then used to inoculate a growth fermentor. The growth fermentor will usually be of a larger size than seed reactor. Acetogenic bacteria in the growth reactor are then grown to a desired cell density. The growth reactor may then be used to inoculate another larger growth reactor or may be used to inoculate a main reactor. The main reactor will be of a larger size than the growth reactor. The use of multiple reactors increases start-up times and increases costs.

SUMMARY

Methods and apparatus are provided which are effective for fermentation of syngas. The bioreactor may include a growth fermentor section and a main fermentor section. The inclusion of a growth fermentor as a continuous part of a main reactor allows for a reduction in the number of separate growth fermentors, which may decrease start-up time and decrease equipment count and costs.

A bioreactor is provided that includes a main reactor having a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor. The bioreactor also includes a growth reactor continuous with the main reactor and having a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor. In this aspect the main reactor volume to growth reactor volume is about 10:1 to about 100:1.

In another aspect, a start-up process is provided that includes contacting acetogenic bacteria with syngas in a growth fermentor section of a reactor vessel for a time effective for providing a cell density of at least about 3 grams per liter. Upon attaining a cell density of at least about 3 grams per liter, medium is added to the reactor vessel to reach a liquid level in the reactor vessel. Medium is added at a rate effective for maintaining a cell density of at least about 3 grams per liter during medium addition. In this aspect, the acetogenic bacteria are contacted with the syngas in a growth reactor section of the reactor vessel which is continuous with a main reactor section of the reactor vessel. The growth reactor section includes a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor. The main reactor section includes a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor.

In another aspect, a start-up process is provided that includes contacting acetogenic bacteria with syngas in a reactor vessel for a time effective for providing a cell density of at least about 5 grams per liter. Upon reaching a cell density of about 5 grams per liter, medium is added to reach a liquid level in the reactor vessel. In this aspect, the acetogenic bacteria are contacted with the syngas in a growth reactor section of the reactor vessel which is continuous with a main reactor section of the reactor vessel. The growth reactor section includes a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor. The main reactor section includes a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor.

In another aspect, a process for fermentation of syngas is provided. The process includes contacting acetogenic bacteria with syngas in a growth section of a reactor vessel for a time effective for providing a cell density of at least about 3 grams per liter. Medium is added to the reactor vessel while maintaining a cell density of at least about 3 grams per liter until reaching a liquid level in a main section of the reactor vessel. In this aspect, the growth section and main section of the reactor vessel are continuous. Syngas is introduced into the main section of the reactor vessel through a gas sparger at a flow rate effective for maintaining a pressure inside of the reactor vessel of at least about 1 psig. The syngas has a CO/CO₂ molar ratio of at least about 0.75. An agitation energy input of about 0.01 to about 12 kWatts/m³ medium is provided to the main section of the reactor vessel. The process is effective for providing a volumetric CO mass transfer coefficient of about 100 to about 1500 per hour and an STY of at least 10 g ethanol/(L•day).

BRIEF DESCRIPTION OF FIGURES

The above and other aspects, features and advantages of several aspects of the process will be more apparent from the following drawings.

FIG. 1 is a perspective view of a bioreactor.

FIG. 2 illustrates an alternative configuration of a bioreactor.

FIGS. 3A and 3B illustrate a bottom view of a gas inlet/sparger.

FIG. 4 is a cross sectional view of a gas sparger.

FIGS. 5A and 5B are top cross sectional views of a reactor vessel showing different impeller assemblies.

FIG. 6 illustrates an alternative configuration of the bioreactor growth fermentor section.

Corresponding reference characters indicate corresponding components throughout the several views of the drawings. Skilled artisans will appreciate that elements in the figures are illustrated for simplicity and clarity and have not necessarily been drawn to scale. For example, the dimensions of some of the elements in the figures may be exaggerated relative to other elements to help to improve understanding of various aspects of the present process and apparatus. Also, common but well-understood elements that are useful or necessary in commercially feasible aspects are often not depicted in order to facilitate a less obstructed view of these various aspects.

DETAILED DESCRIPTION

The following description is not to be taken in a limiting sense, but is made merely for the purpose of describing the general principles of exemplary embodiments. The scope of the invention should be determined with reference to the claims.

Syngas fermentation efficiency is improved by enhancing conditions for increasing the volumetric CO mass transfer coefficient. Methods and apparatus are provided that are effective for providing a volumetric CO mass transfer coefficient of about 100 to about 1500 per hour, in another aspect, about 200 to about 1100 per hour, in another aspect, about 200 to about 900 per hour, in another aspect, about 300 to about 800 per hour, in another aspect, about 400 to about 700 per hour, and in another aspect about 500 to about 600 per hour. Variables which affect the CO mass transfer coefficient include syngas sparging, reactor vessel pressure, syngas quality, and gas dispersion and mixing.

The processes described herein are effective for providing a high level of productivity. In this aspect, the process is effective for providing a STY (space time yield) of at least about 10 g ethanol/(L•day). Possible STY values include about 10 g ethanol/(L•day) to about 200 g ethanol/(L•day), in another aspect, about 10 g ethanol/(L•day) to about 160 g ethanol/(L•day), in another aspect, about 10 g ethanol/(L•day) to about 120 g ethanol/(L•day), in another aspect, about 10 g ethanol/(L•day) to about 80 g ethanol/(L•day), in another aspect, about 20 g ethanol/(L•day) to about 140 g ethanol/(L•day), in another aspect, about 20 g ethanol/(L•day) to about 100 g ethanol/(L•day), in another aspect, about 40 g ethanol/(L•day) to about 140 g ethanol/(L•day), and in another aspect, about 40 g ethanol/(L•day) to about 100 g ethanol/(L•day).

DEFINITIONS

Unless otherwise defined, the following terms as used throughout this specification for the present disclosure are defined as follows and can include either the singular or plural forms of definitions below defined:

The term “about” modifying any amount refers to the variation in that amount encountered in real world conditions, e.g., in the lab, pilot plant, or production facility. For example, an amount of an ingredient or measurement employed in a mixture or quantity when modified by “about” includes the variation and degree of care typically employed in measuring in an experimental condition in production plant or lab. For example, the amount of a component of a product when modified by “about” includes the variation between batches in a multiple experiments in the plant or lab and the variation inherent in the analytical method. Whether or not modified by “about,” the amounts include equivalents to those amounts. Any quantity stated herein and modified by “about” can also be employed in the present disclosure as the amount not modified by “about”.

“Carbonaceous material” as used herein refers to carbon rich material such as coal, and petrochemicals. However, in this specification, carbonaceous material includes any carbon material whether in solid, liquid, gas, or plasma state. Among the numerous items that can be considered carbonaceous material, the present disclosure contemplates: carbonaceous material, carbonaceous liquid product, carbonaceous industrial liquid recycle, carbonaceous municipal solid waste (MSW or msw), carbonaceous urban waste, carbonaceous agricultural material, carbonaceous forestry material, carbonaceous wood waste, carbonaceous construction material, carbonaceous vegetative material, carbonaceous industrial waste, carbonaceous fermentation waste, carbonaceous petrochemical co products, carbonaceous alcohol production co-products, carbonaceous coal, tires, plastics, waste plastic, coke oven tar, fibersoft, lignin, black liquor, polymers, waste polymers, polyethylene terephthalate (PETA), polystyrene (PS), sewage sludge, animal waste, crop residues, energy crops, forest processing residues, wood processing residues, livestock wastes, poultry wastes, food processing residues, fermentative process wastes, ethanol co-products, spent grain, spent microorganisms, or their combinations.

The term “fibersoft” or “Fibersoft” or “fibrosoft” or “fibrousoft” means a type of carbonaceous material that is produced as a result of softening and concentration of various substances; in an example carbonaceous material is produced via steam autoclaving of various substances. In another example, the fibersoft can include steam autoclaving of municipal, industrial, commercial, and medical waste resulting in a fibrous mushy material.

The term “municipal solid waste” or “MSW” or “msw” means waste that may include household, commercial, industrial and/or residual waste.

The term “syngas” or “synthesis gas” means synthesis gas which is the name given to a gas mixture that contains varying amounts of carbon monoxide and hydrogen. Examples of production methods include steam reforming of natural gas or hydrocarbons to produce hydrogen, the gasification of coal and in some types of waste-to-energy gasification facilities. The name comes from their use as intermediates in creating synthetic natural gas (SNG) and for producing ammonia or methanol. Syngas comprises use as an intermediate in producing synthetic petroleum for use as a fuel or lubricant via Fischer-Tropsch synthesis and previously the Mobil methanol to gasoline process. Syngas consists primarily of hydrogen, carbon monoxide, and some carbon dioxide, and has less than half the energy density (i.e., BTU content) of natural gas. Syngas is combustible and is often used as a fuel source or as an intermediate for the production of other chemicals.

The terms “fermentation”, fermentation process” or “fermentation reaction” and the like are intended to encompass both the growth phase and product biosynthesis phase of the process. In one aspect, fermentation refers to conversion of CO to alcohol.

The term “mass transfer” as used herein relates to the transfer of atoms or molecules, particularly substrate atoms or molecules from a gaseous phase into an aqueous solution. A mass transfer coefficient may be calculated in accordance with the equations described in Younesi et al. (Iranian Journal of Biotechnology, Vol. 4, No. 1, January 2006), which is incorporated herein by reference. The following equation represents CO bioconversion (X_co) and the volumetric mass transfer coefficient:

$\frac{X_{\mathrm{CO}}}{1-X_{\mathrm{CO}}}=\frac{{\mathrm{RTV}}_L\left(k_La\right)}{\pi {\mathrm{Hv}}_g}$

• • k_La: volumetric mass transfer coefficient
  • X_co: % CO bioconversion
  • R: constant
  • T: temperature
  • V_L: liquid volume
  • H: Henry's constant (CO=1.226 liter•atm•mmol⁻¹)
  • v_g: gas volume

The term “increasing the efficiency”, “increased efficiency” and the like, when used in relation to a fermentation process includes increasing one or more of the rate of growth of microorganisms in the fermentation, the volume or mass of desired product (such as alcohols) produced per volume or mass of substrate (such as carbon monoxide) consumed, the rate of production or level of production of the desired product, and the relative proportion of the desired product produced compared with other by-products of fermentation.

Bioreactor Design

FIG. 1 is a perspective view of a bioreactor apparatus. The bioreactor apparatus includes a housing 105 defining a main reactor vessel 100. The main reactor vessel 100 may be substantially cylindrical and a cross section of the reactor vessel may be shaped in the form of a circle, substantially circular, or other shapes that are effective for improving mixing and mass transfer. The housing 105 may be formed of any materials know to withstand operating pressures of at least about 1 psig and up to pressures of at least about 250 psig and which is compatible with medium. In various aspects, the following pressures may be utilized, about 5 to about 200 psig, about 5 to about 100 psig, about 5 to about 50 psig, about 5 to about 25 psig, about 10 to about 200 psig, about 10 to about 100 psig, about 10 to about 50 psig, about 10 to about 25 psig, about 15 to about 200 psig, about 15 to about 100 psig, about 15 to about 50 psig, about 15 to about 25 psig, about 20 to about 200 psig, about 20 to about 100 psig, about 20 to about 50 psig, and about 20 to about 25 psig, Some examples of suitable materials include stainless steel, steel with a suitable inner liner and glass.

As further shown in FIG. 1, syngas enters the main reactor vessel 100 through a gas inlet/distributor/sparger 120. Dispersion of the syngas and further mixing is accomplished with at least one gas dispersion impeller 225 and at least one mixing impeller 220 which are coupled to a drive shaft 200. The drive shaft 200 is supported by an agitator support plate 210. Gas is exhausted from the main reactor vessel 100 through exhaust valve 170. The main reactor vessel 100 may also include baffles 300 to further enhance mixing. In this aspect, the baffles 300 may be extended about 25% above an ungassed liquid level 115 to allow for a higher operating liquid level if the system is found to have low foaming.

In another aspect, the main reactor vessel 100 may include addition ports 230. The addition ports 230 may include for example, one or more acidic addition ports, one or more alkaline addition ports, and one or more nutrient addition ports. In this aspect, the addition ports may be equally spaced apart around a circumference of the reaction vessel. The ports may be on the same or different horizontal plane. In one aspect, the main reactor vessel 100 includes at least 4 equally spaced medium addition ports adjacent to a mixing impeller 220. The ports may be spaced around a circumference of the main reactor vessel 100 at angles of 45° apart.

A gassed liquid level 110 and an ungassed liquid level 115 are maintained in the main reactor vessel 100. Maintaining an ungassed liquid level 115 in the main reactor vessel 100 allows for more efficient mass transfer and helps in maintaining control of foaming. In this aspect, an ungassed liquid level 115 is maintained in the main reactor vessel 100 which is effective for providing a head space of at least about 1% of a total volume of the main reactor vessel 100. In another aspect, the ungassed liquid level 115 provides a head space of about 1 to about 75% of a total volume of the main reactor vessel 100. In various aspects, the head space may include the following percentages of the total volume of the reactor: about 5 to about 50%, about 10 to about 50%, about 15 to about 50%, about 20 to about 50%, about 25 to about 50%, about 30 to about 50%, about 30 to about 40% and about 30 to about 35%. The main reactor vessel 100 may also include at least one liquid inlet 130 which aids in controlling foaming and allows for adjustment in reactor liquid volume. The liquid inlet 130 may be in the form of a spray nozzle. The main reactor vessel 100 may also include additional ports 190.

As further illustrated in FIG. 1, the main reactor vessel 100 may be continuous with a growth reactor section 400. A vortex breaker 410 may be disposed within the growth reactor section and over a medium outlet 420. The growth reactor section 400 and vortex breaker 410 are effective for preventing gas from being drawn out through the medium outlet 420. Medium drawn out through medium outlet 420 may be sent to a medium to recycle loop 450 or to a medium filter loop 460. Medium from the medium recycle loop 450 may be sent to a cooler/heat exchanger 500 and cooled medium 510 may be cycled back to the reactor vessel 100. In this aspect, the main reactor volume to growth reactor volume is about 10:1 to about 100:1, in another aspect, about 10:1 to about 75:1, in another aspect about 10:1 to about 50:1, in another aspect, about 10:1 to about 40:1, in another aspect about 10:1 to about 30:1, in another aspect, about 15:1 to about 50:1, in another aspect about 15:1 to about 40:1, in another aspect, about 15:1 to about 30:1, in another aspect about 16: to about 25:1.

During operation of the main reactor, the growth reactor 400 may be utilized as a gas/liquid disengagement zone which is effective for allowing gas bubbles to rise from the growth reactor 400 back into the main reactor vessel 100. In this aspect, liquid in the growth reactor section 400 should be as undisturbed as possible during operation of the main reactor 100. Gas bubbles must rise out of the growth reactor section 400 faster than liquid is drawn down. In this aspect, less than about 2% gas is drawn through the medium outlet 420 to a pump. The main reactor volume to growth reactor volume is about 10:1 to about 100:1.

Medium from the medium filter loop 460 may be sent to a recycle filter 600. Concentrated cells 610 are returned to the main reactor vessel 100 and permeate 620 is sent for further processing. Further processing may include separation of desired product such as for example ethanol, acetic acid and butanol.

In another aspect, the bioreactor may be configured without impellers. For example, the bioreactor may be configured as a trickle bed reactor (TBR), cocurrent contactor (CCC), a bubble column type reactor, or moving bed bioreactors (MBBR). In these reactor configurations, an agitation energy of about 0.01 to about 12 kWatts/m³ medium is provided. Some examples of cocurrent contactor (CCC) include cocurrent downflow contactor (CDC) which are further illustrated in U.S. Pat. Nos. 4,834,343 and 5,286,466, which are both incorporated herein by reference. An example of moving bed bioreactors (MBBR) is provided in U.S. Publication No. 2009/0035848, which is incorporated herein by reference.

FIG. 2 illustrates an alternative reactor configuration where the main reactor is a bubble column type reactor 800. The bubble column reactor can be a slurry bubble column, packed bubble column, or tray bubble column. As illustrated in FIG. 2, the bubble column reactor 800 is a multistage bubble column and may include any type of internal column arrangements 700 known in the art. Bubble columns may also include loop reactors which may include airlift loop reactors, propeller loop reactors, and jet loop reactors. Some examples of bubble column type reactors are provided in U.S. Pat. Nos. 7,309,599, 6,440,712, and 5,242,643, and in Shah et al., AIChE Journal, Vol. 28, Issue 3, pages 353-379 (1982), and Chang et al., Process Biochemistry, Vol. 37, Issue 4, pages 411-421 (2001), all of which are incorporated herein by reference.

Syngas and Syngas Sparging

Syngas is introduced into the bioreactor 100 through a gas inlet/sparger 120. Syngas may be provided from any know source. In one aspect, syngas may be sourced from gasification of carbonaceous materials. Gasification involves partial combustion of biomass in a restricted supply of oxygen. The resultant gas mainly includes CO and H₂. In this aspect, syngas will contain at least about 20 mole % CO, in one aspect, about 20 to about 100 mole % CO, in another aspect, about 30 to about 90 mole % CO, in another aspect, about 40 to about 80 mole % CO, and in another aspect, about 50 to about 70 mole % CO. The syngas will have a CO/CO₂ molar ratio of at least about 0.75. Some examples of suitable gasification methods and apparatus are provided in U.S. Ser. Nos. 61/516,667, 61/516,704 and 61/516,646, all of which were filed on Apr. 6, 2011, and all of which are incorporated herein by reference.

The bioreactor may include a CO concentration gradient where the CO concentration near the sparger is higher than the CO concentration at a higher level of the bioreactor. In this aspect, the bioreactor includes a ratio of CO concentration at a bottom level (sparger level) of the bioreactor to CO concentration at a top level of the bioreactor of about 100:1 to about 10:1.

One factor that may affect the mass transfer rate of the CO into the aqueous medium is the partial pressure of the gaseous substrate that includes the CO. In this aspect, the mass transfer rate can be increased by increasing the proportion of CO in a gas stream by enrichment or removal of unwanted components. In this aspect, the gas stream will have less than about 10 ppm oxygenated or non-oxygenated aromatics.

FIGS. 3A and 3B illustrate a bottom view of a gas inlet/sparger 120. In this aspect, the gas inlet/sparger 120 may include an inlet conduit 530 which is continuous with a sparger assembly 540. The sparger assembly 540 may be generally annular or circular as shown, or may be any other shape, such as for example, a straight, rectangular or free form. In the aspect where the sparger assembly 540 is annular in shape, the sparger assembly 540 has a diameter that is about 30 to about 100% of a diameter formed by the gas dispersion impellers 225, in various other aspects, about 40 to about 90%, about 40 to about 80%, and about 50 to about 70%.

The bottom portion of the gas sparger assembly 540 may include a plurality of holes 550. The holes 550 are of a diameter effective for providing a gas velocity of about 25 m/sec or greater at an exit of the holes, in another aspect, a gas velocity of about 25 m/sec to about 75 m/sec at an exit of the holes. In various aspects, the gas velocity may include the following ranges: about 25 to about 75 m/sec, about 25 to about 50 m/sec, about 25 to about 40 m/sec, about 25 to about 30 m/sec, about 30 to about 75 m/sec, about 30 to about 50 m/sec, about 30 to about 40 m/sec, about 35 to about 75 m/sec, about 35 to about 50 m/sec, about 35 to about 40 m/sec, about 40 to about 75 m/sec, about 40 to about 50 m/sec, and about 50 to about 75 m/sec. In this aspect, the holes will have a diameter of about 10 mm or less and in another aspect, a diameter of about 2.5 mm to about 1.0 mm.

FIG. 4 illustrates a cross sectional view of a sparger assembly 540. In this aspect, dotted arrow lines show the flow of gas through hole 550. An angle of 120° is shown with lines drawn to a midpoint of the sparger assembly (shown as α). Holes may be located at any angle along the sparger assembly. In one aspect, the sparger assembly 540 includes about 1 to about 5 rows of parallel holes 550. Holes 550 are spaced apart and point in a downward direction. As shown in FIG. 4, the sparger assembly 540 includes 5 parallel rows of holes 550 and a total number of 790 holes spaced 30° apart. The downward pointing direction of the holes is effective for preventing fouling or clogging of the holes and helps to minimize back flow into the sparger assembly 540.

Gas Dispersion and Mixing

Referring again to FIG. 1, the reactor vessel 100 further includes a mixing assembly that includes a drive shaft 200, at least one mixing impeller 220, and at least one gas dispersion impeller 225. The mixing impeller 220 will generally be located below the liquid level 110. In one aspect, the reactor vessel 100 includes two or more mixing impellers 220. A gas dispersion impeller 225 is located below the mixing impeller 220. The reactor vessel 100 may include one or two or more gas dispersion impellers 225.

Referring now to FIG. 5A, each mixing and gas dispersion impeller assembly includes a hub 500 and a group of impellers arranged around the drive shaft 200. Each impeller includes an arm 510 attached to the hub 500 and holding one or more blades 520. The blades may be either mixing impeller or gas dispersion impellers. The mixing impeller assembly includes at least 2 blades and may include up to 6 blades. Examples of mixing impeller include low energy impellers such as marine impellers or marine propellers. In another aspect, the gas dispersion impeller assembly includes at least 2 blades and may include up to 6 blades. Examples of gas dispersion impellers include high energy impellers such as Rushton impellers or concave impellers. FIG. 5A is similar to FIG. 5B except that the blades 520 are attached directly to a hub 500.

Upon rotation of the drive shaft 200, syngas introduced through the gas inlet/sparger is entrained in small bubbles in the medium and travels around the generally circular cross section of the reactor vessel 100. The drive shaft is operably connected to and may be rotated with any suitable agitator, such as for example, an electric motor, a motor and gearbox, or a hydraulic motor. In this aspect, the agitator provides an energy input of about 0.3 to about 12 kWatts/m³, in another aspect, about 0.7 kWatts/m³ to about 12 kWatts/m³, and in an important aspect, 0.9 kWatts/m³ to about 12 kWatts/m³ medium.

Bioreactor Operation

In accordance with one aspect, the fermentation process is started by addition of a suitable medium to the reactor vessel. The liquid contained in the reactor vessel may include any type of suitable nutrient medium or fermentation broth. The nutrient medium will include vitamins and minerals effective for permitting growth of the microorganism being used. Anaerobic medium suitable for the fermentation of ethanol using CO as a carbon source are known. One example of a suitable fermentation medium is described in U.S. Pat. No. 7,285,402, which is incorporated herein by reference.

The medium is sterilized to remove undesirable microorganisms and the reactor is inoculated with the desired microorganisms. In one aspect, the microorganisms utilized include acetogenic bacteria. Examples of useful acetogenic bacteria include those of the genus Clostridium, such as strains of Clostridium ljungdahlii, including those described in WO 2000/68407, EP 117309, U.S. Pat. Nos. 5,173,429, 5,593,886 and 6,368,819, WO 1998/00558 and WO 2002/08438, strains of Clostridium autoethanogenum (DSM and DSM 19630 of DSMZ, Germany) including those described in WO 2007/117157 and WO 2009/151342 and Clostridium ragsdalei (P11, ATCC BAA-622) and Alkalibaculum bacchi (CP11, ATCC BAA-1772) including those described respectively in U.S. Pat. No. 7,704,723 and “Biofuels and Bioproducts from Biomass-Generated Synthesis Gas”, Hasan Atiyeh, presented in Oklahoma EPSCoR Annual State Conference, Apr. 29, 2010 and Clostridium carboxidivorans (ATCC PTA-7827) described in U.S. Patent Application No. 2007/0276447. Other suitable microorganisms includes those of the genus Moorella, including Moorella sp. HUC22-1, and those of the genus Carboxydothermus. Each of these references is incorporated herein by reference. Mixed cultures of two or more microorganisms may be used.

Some examples of useful bacteria include Acetogenium kivui, Acetoanaerobium noterae, Acetobacterium woodii, Alkalibaculum bacchi CP11 (ATCC BAA-1772), Blautia producta, Butyribacterium methylotrophicum, Caldanaerobacter subterraneous, Caldanaerobacter subterraneous pacificus, Carboxydothermus hydrogenoformans, Clostridium aceticum, Clostridium acetobutylicum, Clostridium acetobutylicum P262 (DSM 19630 of DSMZ Germany), Clostridium autoethanogenum (DSM 19630 of DSMZ Germany), Clostridium autoethanogenum (DSM 10061 of DSMZ Germany), Clostridium autoethanogenum (DSM 23693 of DSMZ Germany), Clostridium autoethanogenum (DSM 24138 of DSMZ Germany), Clostridium carboxidivorans P7 (ATCC PTA-7827), Clostridium coskatii (ATCC PTA-10522), Clostridium drakei, Clostridium ljungdahlii PETC (ATCC 49587), Clostridium ljungdahlii ER12 (ATCC 55380), Clostridium ljungdahlii C-01 (ATCC 55988), Clostridium ljungdahlii O-52 (ATCC 55889), Clostridium magnum, Clostridium pasteurianum (DSM 525 of DSMZ Germany), Clostridium ragsdali P11 (ATCC BAA-622), Clostridium scatologenes, Clostridium thermoaceticum, Clostridium ultunense, Desulfotomaculum kuznetsovii, Eubacterium limosum, Geobacter sulfurreducens, Methanosarcina acetivorans, Methanosarcina barkeri, Morrella thermoacetica, Morrella thermoautotrophica, Oxobacter pfennigii, Peptostreptococcus productus, Ruminococcus productus, Thermoanaerobacter kivui, and mixtures thereof.

Upon inoculation, an initial feed gas supply rate is established effective for supplying the initial population of microorganisms. Effluent gas is analyzed to determine the content of the effluent gas. Results of gas analysis are used to control feed gas rates. Upon reaching desired levels, liquid phase and cellular material is withdrawn from the reactor and replenished with medium. In this aspect, the bioreactor is operated to maintain a cell density of at least about 2 grams/liter, and in another aspect, about 2 to about 50 grams/liter, in various other aspects, about 5 to about 40 grams/liter, about 5 to about 30 grams/liter, about 5 to about 20 grams/liter, about 5 to about 15 grams/liter, about 10 to about 40 grams/liter, about 10 to about 30 grams/liter, about 10 to about 20 grams/liter, and about 10 to about 15 grams/liter. Cell density may be controlled through the recycle filter 600. In a related aspect, the bioreactor is operated to provide a liquid retention time of about 10 to about 400 hours, and in various aspect, about 10 to about 300 hours, about 10 to about 200 hours, about 10 to about 100 hours, about 10 to about 75 hours, about 10 to about 60 hours, about 10 to about 50 hours, about 10 to about 40 hours, about 10 to about 30 hours, and about 10 to about 20 hours. In this aspect, liquid retention time (LRT) may be calculated as follows:

$\mathrm{LRT}=\frac{\mathrm{liquid}\mathrm{volume}}{\mathrm{net}\mathrm{liquid}\mathrm{volume}\mathrm{flow}\mathrm{rate}\left(\mathrm{in}\mathrm{or}\mathrm{out}\right)}$

Syngas is introduced into the bioreactor at a rate effective for maintaining a pressure in the bioreactor of at least about 1 psig, and in another aspect, a pressure of about 10 to about 250 psig. In various other aspect, the pressure may be about 10 to about 200 psig, about 10 to about 100 psig, about 10 to about 75 psig, about 10 to about 50 psig, about 10 to about 25 psig, about 20 to about 250 psig, about 20 to about 200 psig, about 20 to about 100 psig, about 20 to about 75 psig, about 20 to about 50 psig, about 20 to about 25 psig, about 30 to about 250 psig, about 30 to about 200 psig, about 30 to about 100 psig, about 30 to about 75 psig, about 30 to about 50 psig, about 40 to about 250 psig, about 40 to about 200 psig, about 40 to about 100 psig, about 40 to about 75 psig, about 40 to about 50 psig, about 50 to about 250 psig, about 50 to about 200 psig, about 50 to about 100 psig, and about 50 to about 75 psig.

In one aspect, in certain size fermentors, syngas is introduced into the gas inlet/sparger 120 at a rate of about 10 to about 50 ft³/sec, and in another aspect, a rate of about 25 to about 35 ft³/sec. Pressure is controlled through controlling the rate at which syngas is introduced in combination with controlling the rate at which gas is exhausted from the reaction vessel. Pressure may be measured in the reactor headspace or at the bottom of the reactor vessel.

In one aspect, sparger holes 550 and a pressure drop across the hole is important for improving the volumetric mass transfer rate of CO. A pressure drop across sparger holes 550 needs to be high enough to ensure distribution of gas bubble around the sparger assembly 540. In this aspect, sparging is effective to provide a pressure drop across the sparger holes 550 of about 0.5 psi to about 2.5 psi, and in another aspect about 1 psi to about 2 psi. The sparger holes 550 provide advantages over other forms of sparging. For example, sparger holes 550 are effective for avoiding fouling, as may occur with sintered metal spargers. Further, the sparger holes 550 are effective for providing consistent gas bubble sizes which contribute towards improved mass transfer.

Another factor that may affect the mass transfer rate is gas retention time. In this aspect, the bioreactor is effective for providing a gas retention time of at least about 2 minutes, and in another aspect, a gas retention time of about 2 minutes to about 15 minutes, in and in another aspect about 5 to about 10 minutes. Gas retention time (GRT) may be determined according to the following formula:

$\mathrm{GRT}=\frac{\mathrm{liquid}\mathrm{volume}}{\mathrm{gas}\mathrm{flow}\mathrm{rate}\left(\mathrm{in}\mathrm{or}\mathrm{out}\right)}$

Temperature and ionic strength may also have an affect on the mass transfer rate. In this aspect, the temperature of the bioreactor is about 30 to about 50° C.

An alternative configuration of the growth reactor 400 is shown in FIG. 6. In this aspect, the growth reactor 400 is utilized as a growth reactor during startup. The growth reactor 400 is configured to include a growth reactor sparger 600. The growth reactor 400 may be configured with any known mixing apparatus. For example, gas mixing may be effected with impellers (not shown) such as with a stirred tank reactor, or with a gas lift type fermentor equipped with a draft tube 620. As shown in FIG. 6, the gas lift fementor is effective for circulating bubbles 610 and cells around the growth fermentor 400. In this aspect, bubbles 610 rising in a draft tube 620 cause mixing. The motion of the gas carries fluid and cells up the draft tube 620. At the top, gas leaves the liquid and the degas sed liquid (which is heavier than the gassed liquid) descends in the ring outside the draft tube. At the bottom of the reactor, the descending fluid encounters the gas stream and is carried back up the draft tube 620. Other reactor designs may include a bubble type reactor, trickle bed reactor (TBR), and cocurrent reactor (CCC). Reactors may include an external gas loop or jet type reactors may be utilized.

The growth reactor is utilized by inoculating acetogenic bacteria into a medium contained in the growth reactor section 400 of a reactor vessel. The medium in the growth reactor 400 fills at least about 75% of a total volume of the growth reactor, in another aspect at least about 80%, in another aspect at least about 85%, in another aspect at least about 90%, and in another aspect at least about 95%. The growth reactor is sparged with syngas and mixed for a time effective to provide a target cell density. In one aspect, the target cell density will be about 5 to about 40 grams/liter, and in various other aspects, about 5 to about 30 grams/liter, about 5 to about 20 grams/liter, about 5 to about 15 grams/liter, about 10 to about 40 grams/liter, about 10 to about 30 grams/liter, about 10 to about 20 grams/liter, and about 10 to about 15 grams/liter. Upon reaching a target cell density, medium levels are allowed to rise out the growth reactor and into the main reactor vessel to previously indicated levels. Sparging and mixing in the growth reactor is stopped and the fermentation proceeds as previously described.

In another aspect, the cell density in the growth reactor may be brought to a level of at least about 3 grams per liter or any of the cell densities described herein. Upon reaching a cell density of at least about 3 grams per liter, medium is added at a rate effective to allow the cell density level to remain at a level of at least about 3 grams per liter. Upon reaching a desired medium level, sparging and mixing in the growth reactor is stopped and the fermentation proceeds as previously described.

While the invention herein disclosed has been described by means of specific embodiments, examples and applications thereof, numerous modifications and variations could be made thereto by those skilled in the art without departing from the scope of the invention set forth in the claims.

Claims

1. A bioreactor comprising:

a main reactor having a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor, wherein a portion of the main reactor is utilized as a growth reactor.

2. A bioreactor comprising:

a main reactor having a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR); and

a growth reactor continuous with the main reactor and having a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor.

3. The bioreactor of claim 1 or 2 wherein the main reactor is configured as a stirred tank reactor.

4. The bioreactor of claim 3 wherein agitation in the main reactor is provided by one or more of a mechanical agitator, gas injection, liquid injection, and liquid recirculation (pump around).

5. The bioreactor of claim 3 wherein the main reactor includes a mechanical agitator operably connected to a drive shaft.

6. The bioreactor of claim 5 wherein at least one mixing impeller is operably connected to the drive shaft and at least one gas dispersion impeller is operably connected to the drive shaft and disposed below the gas dispersion impeller.

7. The bioreactor of claim 6 further comprising a gas sparger disposed below the gas dispersion impeller.

8. The bioreactor of claim 7 wherein the gas sparger includes holes having a diameter of 10 mm or less.

9. The bioreactor of claim 2 wherein the main reactor includes a draft tube.

10. The bioreactor of claim 2 wherein the growth reactor is unstirred.

11. The bioreactor of claim 2 wherein the growth reactor is a stirred tank reactor.

12. The bioreactor of claim 2 wherein the growth reactor is stirred by a liquid recirculation (pump-round).

13. The bioreactor of claim 2 wherein the growth reactor is stirred by gas lift.

14. The bioreactor of claim 2 wherein the growth reactor includes a draft tube.

15. The bioreactor of claim 2 wherein the main reactor volume to growth reactor volume is about 10:1 to about 100:1.

16. A process comprising:

contacting acetogenic bacteria with syngas in a reactor vessel for a time effective for providing a cell density of at least about 3 grams per liter; and

adding medium to the reactor vessel to reach a liquid level in the reactor vessel, wherein the cell density of at least about 3 grams per liter is maintained while adding medium.

17. The process of claim 16 wherein the acetogenic bacteria are contacted with the syngas in a growth reactor section of the reactor vessel, the growth reactor section of the reactor vessel being continuous with a main reactor section of the reactor vessel.

18. The process of claim 17 wherein the growth reactor section includes a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor.

19. The process of claim 17 wherein the main reactor section includes a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor.

20. The process of claim 17 wherein the process is effective for providing a substantially uniform concentration of CO in the main reactor section.

21. The process of claim 17 wherein the process is effective for providing a CO concentration substantially higher at a bottom portion of the main reactor section as compared to an upper portion of the main reactor section.

22. A process comprising:

contacting acetogenic bacteria with syngas in a reactor vessel for a time effective for providing a cell density of at least about 5 grams per liter; and

adding medium to the reactor vessel to reach a liquid level in the reactor vessel.

23. The process of claim 22 wherein the acetogenic bacteria are contacted with the syngas in a growth reactor section of the reactor vessel, the growth reactor section of the reactor vessel being continuous with a main reactor section of the reactor vessel.

24. The process of claim 23 wherein the growth reactor section includes a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor.

25. The process of claim 23 wherein the main reactor section includes a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor.

26. The process of claim 22 or 23 wherein the process is effective for providing a substantially uniform concentration of CO in the main reactor section.

27. The process of claim 22 or 23 wherein the process is effective for providing a CO concentration substantially higher at a bottom portion of the main reactor section as compared to an upper portion of the main reactor section.

28. The process of claim 22 or 23 wherein the ratio of CO concentration at a bottom portion of the reactor to the concentration at an upper portion of the reactor is about 100:1 to about 10:1.

29. A process for fermentation of syngas, the process comprising:

contacting acetogenic bacteria with syngas in a growth section of a reactor vessel for a time effective for providing a cell density of at least about 3 grams per liter;

adding medium to the reactor vessel and maintaining a cell density of at least about 3 grams per liter until reaching a liquid level in a main section of the reactor vessel, wherein the growth section and main section of the reactor vessel are continuous;

introducing syngas into the main section of the reactor vessel through a gas sparger, the syngas being introduced at a flow rate effective for maintaining a pressure inside of the reactor vessel of at least about 1 psig, wherein the syngas has a CO/CO2 molar ratio of at least about 0.75; and

providing an agitation energy input to the main section of the reactor vessel of about 0.01 to about 12 kWatts/m3 medium,

wherein the process is effective for providing a volumetric CO mass transfer coefficient of about 100 to about 1500 per hour.

30. The process of claim 29 wherein the growth reactor section includes a configuration selected from the group consisting of stirred and unstirred tank reactor, trickle bed reactor (TBR), cocurrent contactor (CCC), moving bed bioreactor (MBBR), and a bubble column reactor.

31. The process of claim 29 wherein the gas sparger includes holes having a diameter of 10 mm or less.

32. The process of claim 29 wherein the syngas pressure drop across the sparger is about 0.5 to about 2.5 psi.

33. The process of claim 29 wherein the process is effective for providing a STY of at least about 10 g ethanol/(L•day).

34. The process of claim 29 wherein the acetogenic bacteria is selected from the group consisting of Acetogenium kivui, Acetoanaerobium noterae, Acetobacterium woodii, Alkalibaculum bacchi CP11 (ATCC BAA-1772), Blautia producta, Butyribacterium methylotrophicum, Caldanaerobacter subterraneous, Caldanaerobacter subterraneous pacificus, Carboxydothermus hydrogenoformans, Clostridium aceticum, Clostridium acetobutylicum, Clostridium acetobutylicum P262 (DSM 19630 of DSMZ Germany), Clostridium autoethanogenum (DSM 19630 of DSMZ Germany), Clostridium autoethanogenum (DSM 10061 of DSMZ Germany), Clostridium autoethanogenum (DSM 23693 of DSMZ Germany), Clostridium autoethanogenum (DSM 24138 of DSMZ Germany), Clostridium carboxidivorans P7 (ATCC PTA-7827), Clostridium coskatii (ATCC PTA-10522), Clostridium drakei, Clostridium ljungdahlii PETC (ATCC 49587), Clostridium ljungdahlii ER12 (ATCC 55380), Clostridium ljungdahlii C-01 (ATCC 55988), Clostridium ljungdahlii O-52 (ATCC 55889), Clostridium magnum, Clostridium pasteurianum (DSM 525 of DSMZ Germany), Clostridium ragsdali P11 (ATCC BAA-622), Clostridium scatologenes, Clostridium thermoaceticum, Clostridium ultunense, Desulfotomaculum kuznetsovii, Eubacterium limosum, Geobacter sulfurreducens, Methanosarcina acetivorans, Methanosarcina barkeri, Morrella thermoacetica, Morrella thermoautotrophica, Oxobacter pfennigii, Peptostreptococcus productus, Ruminococcus productus, Thermoanaerobacter kivui, and mixtures thereof.